JP2015223539A - Water treatment equipment and water treatment method - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide water treatment equipment and a water treatment method capable of efficiently removing soluble silica in water to be treated.SOLUTION: Water treatment equipment 1 includes a soluble silica deposition part 13 in which soluble silica dissolved in water W1 to be treated is deposited from water W1 to be treated having a concentration of aluminate ion expressed by the following formula (1) and pH which are respectively within a predetermined range, a solid-liquid separation part 14 in which the deposited soluble silica is separated from the water W1 to be treated to obtain treated water W1 freed from the soluble silica, from the water W1 to be treated, and a reverse osmosis membrane filtration part 30 in which the treated water W1 freed from the soluble silica on the solid-liquid separation part 14 is filtered by a reverse osmosis membrane 30a: [Al(OH)]... formula (1).

Description

  The present invention relates to a water treatment apparatus and a water treatment method, and more particularly to a water treatment apparatus and a water treatment method capable of efficiently removing soluble silica in water to be treated.

  Conventionally, a wastewater treatment method for removing soluble silica from wastewater discharged in a chemical / mechanical polishing (CMP) process of a semiconductor device manufacturing process has been proposed (see, for example, Patent Document 1). In this wastewater treatment method, wastewater containing soluble silica is treated with a coagulant to aggregate the soluble silica, and then the aggregated soluble silica is removed with a microfiltration membrane. Then, by periodically flushing the microfiltration membrane, the soluble silica in the water to be treated is removed as a solid from the membrane surface of the microfiltration membrane.

US Pat. No. 5,904,853

  However, in the wastewater treatment method described in Patent Document 1, since the coagulant is added and the soluble silica is agglomerated and removed, the concentration of the soluble silica cannot always be sufficiently reduced. In Patent Document 1, a method of removing soluble silica by adding sodium aluminate or the like is also being studied. However, when an aluminum compound is used, the concentration of aluminum in the wastewater increases and reverse osmosis is provided in the subsequent stage. It may adversely affect purification equipment such as membrane equipment.

  This invention is made | formed in view of such a situation, and it aims at providing the water treatment apparatus and water treatment method which can remove the soluble silica in to-be-processed water efficiently.

The water treatment apparatus of the present invention is a solution for precipitating soluble silica dissolved in the water to be treated from the water to be treated whose aluminate ion concentration and pH represented by the following general formula (1) are each within a predetermined range. A solid-liquid separation unit that separates the treated silica precipitation part from the treated water and the precipitated soluble silica to obtain treated water from which the soluble silica has been removed from the treated water, and the solid-liquid separation And a reverse osmosis membrane filtration unit that filters the treated water from which the soluble silica has been removed in the separation unit through a reverse osmosis membrane.
^{_{[Al (OH) 4] -}} ··· formula (1)

  According to this water treatment apparatus, a compound obtained by reacting aluminate ions and soluble silica present in the water to be treated having a predetermined pH is precipitated in the water to be treated, so that the soluble silica is agglomerated using a flocculant. Therefore, it is possible to efficiently remove the soluble silica in the water to be treated as compared with the case of removing it. Therefore, it is possible to realize a water treatment device that can efficiently remove soluble silica in the water to be treated and that can reduce the influence of aluminum ions on the reverse osmosis membrane filtration device.

  The water treatment apparatus of the present invention preferably includes an aluminate ion adding section for adding an aluminate ion additive to the water to be treated.

  In the water treatment apparatus of the present invention, the aluminate ion additive is preferably sodium aluminate.

  In the water treatment apparatus of the present invention, it is preferable to include a pH adjuster addition unit that adds a pH adjuster to the water to be treated to bring the water to be treated to pH 5.5 or more.

  In the water treatment apparatus of the present invention, it is preferable that the water treatment apparatus further includes a seed material addition unit that adds soluble silica contained in the water to be treated, which has been precipitated in advance, as a seed material to the water to be treated.

  In the water treatment apparatus of this invention, it is preferable to provide the magnesium ion addition part which adds a magnesium ion additive to the said to-be-processed water.

  In the water treatment apparatus of the present invention, it is preferable that the apparatus includes an electrolysis apparatus that adds aluminate ion-containing water generated by electrolyzing a part of the treated water to the treated water as the aluminate ion additive. .

The water treatment apparatus of the present invention preferably includes an aluminum ion treatment unit that removes aluminum ions contained in the water to be treated supplied to the reverse osmosis membrane filtration unit.
With this configuration, soluble silica can be removed without using an aluminum-based flocculant, so that the aluminum concentration in the treated water can be reduced.

  In the water treatment apparatus of this invention, it is preferable to remove the said aluminum ion with the ion exchange resin provided in the said aluminum ion processing part.

  In the water treatment apparatus of the present invention, it is preferable to add a chelating agent to the water to be treated in the aluminum ion treatment unit to remove the aluminum ions.

  In the water treatment device of the present invention, based on the aluminum ion concentration measurement device that measures the aluminum ion concentration of the water to be treated introduced into the reverse osmosis membrane filtration unit and the aluminum ion concentration measured by the aluminum ion concentration measurement device. And a controller for controlling at least one of the concentration of the aluminate ions, the pH of the water to be treated, the amount of the chelating agent added to the aluminum ion treatment part, and the treatment of the ion exchange resin. It is preferable.

The water treatment method of the present invention is a method for precipitating soluble silica dissolved in the water to be treated from the water to be treated whose aluminate ion concentration and pH represented by the following general formula (1) are each within a predetermined range. A solid-liquid separation step for obtaining a water to be treated from which the soluble silica is removed from the water to be treated by solid-liquid separation of the water to be treated and the precipitated soluble silica; and the solid-liquid separation. And a filtration step of filtering the treated water from which the soluble silica has been removed by a reverse osmosis membrane filtration unit.
^{_{[Al (OH) 4] -}} ··· formula (1)

  According to this water treatment method, a compound obtained by reacting aluminate ions and soluble silica present in the water to be treated having a pH within a predetermined range is precipitated in the water to be treated, so that the soluble silica is aggregated using a flocculant. Therefore, it is possible to efficiently remove the soluble silica in the water to be treated as compared with the case of removing it. Therefore, it is possible to realize a water treatment method capable of efficiently removing soluble silica in the water to be treated and reducing the influence of aluminum ions on the reverse osmosis membrane filtration device.

  In the water treatment method of the present invention, it is preferable to add an aluminate ion additive to the water to be treated.

  In the water treatment method of the present invention, the aluminate ion additive is preferably sodium aluminate.

  In the water treatment method of the present invention, it is preferable to add a pH adjuster to the water to be treated so that the water to be treated has a pH of 5.5 or more.

  In the water treatment method of the present invention, it is preferable that soluble silica contained in the water to be treated deposited in advance is added to the water to be treated as a seed material.

  In the water treatment method of the present invention, it is preferable to add a magnesium ion additive to the water to be treated.

  In the water treatment method of the present invention, it is preferable to add aluminate ion-containing water generated by electrolyzing a part of the treated water to the treated water as the aluminate ion additive.

  In the water treatment method of the present invention, it is preferable that aluminum ions contained in the water to be treated supplied to the reverse osmosis membrane filtration unit be removed by the aluminum ion treatment unit. By this method, soluble silica can be removed without using an aluminum-based flocculant, so that the aluminum concentration in the treated water can be reduced.

  In the water treatment method of the present invention, the aluminum ion concentration of the water to be treated introduced into the treated water purification unit is measured, and the concentration of the aluminate ion based on the measured aluminum ion concentration, the pH of the water to be treated It is preferable to control at least one of the addition amount of the chelating agent added to the aluminum ion treatment part and the treatment of the ion exchange resin.

  ADVANTAGE OF THE INVENTION According to this invention, the water treatment apparatus and water treatment method which can remove the soluble silica in to-be-processed water efficiently are realizable.

FIG. 1 is a schematic diagram of a water treatment apparatus according to the first embodiment of the present invention. FIG. 2 is a graph showing the relationship between the pH of water to be treated and the solubility of soluble silica in the water to be treated. FIG. 3 is an explanatory diagram showing the solubility of soluble silica in the presence of aluminate ions. FIG. 4A is a diagram showing the relationship between the pH of the water to be treated after the addition of aluminum ions and the concentration of SiO ₂ . FIG. 4B is a diagram showing the relationship between the pH of water to be treated after the addition of aluminum ions and the removal rate of SiO ₂ . FIG. 5 is a diagram showing the relationship between the aluminum addition rate (mol Al / mol SiO ₂ ) and the SiO ₂ removal rate in the water treatment apparatus according to the first embodiment. FIG. 6A is a diagram showing the relationship of the SiO ₂ concentration in the water to be treated after adding magnesium ions. FIG. 6B is a diagram showing the relationship of the removal rate of SiO _{2 in} the water to be treated after the addition of aluminum ions. FIG. 7 is a schematic view of a water treatment apparatus according to the second embodiment of the present invention. FIG. 8 is a schematic view of a water treatment apparatus according to the third embodiment of the present invention. FIG. 9 is a schematic view of the soluble silica removing unit according to the embodiment of the present invention. FIG. 10 is a schematic view of a water treatment apparatus according to the first application example of the present invention. FIG. 11 is a schematic view of a water treatment apparatus according to the second application example of the present invention. FIG. 12 is a schematic view of a water treatment apparatus according to the third application example of the present invention. FIG. 13 is a schematic view of a water treatment apparatus according to the fourth application example of the present invention. FIG. 14 is a diagram showing the results of Examples and Comparative Examples of the present invention.

In cooling water such as cooling towers of plant equipment, a part of the cooling water evaporates due to heat exchange between the high-temperature exhaust gas discharged from the boiler and the cooling water, so that soluble silica (SiO 2 ₂ ) may concentrate and precipitate as scale. For this reason, it is necessary to periodically precipitate and remove the soluble silica contained in the cooling water to keep the concentration of the soluble silica low.

Examples of the method for removing soluble silica in water include an inexpensive aluminum-based flocculant (Al ₂ (SO ₄ ) ₃ ) and polyaluminum chloride ([Al ₂ (OH) nCl ₆ -n] m ^2). )) Is considered. In general, in the coagulation-precipitation treatment, an aluminum-based coagulant is deposited as positively charged aluminum hydroxide (Al (OH) ₃ : solid), and a negatively charged colloid aggregates in the aqueous solution in an aqueous solution. Precipitate. Here, aluminum hydroxide is weakly negatively charged in water at pH 8 or higher, and strongly positively charged at pH 7 or lower. For this reason, the coagulation precipitation using the aluminum-based coagulant is generally carried out at a pH of 7 or less at which aluminum hydroxide is positively charged, not at a pH of 8 or higher at which aluminum hydroxide is negatively charged.

  In the water to be treated having a pH within a predetermined range and an aluminate ion concentration within a predetermined range, and containing soluble silica, the compound of aluminate ions and soluble silica is contained in the water to be treated. We focused on the precipitation. The inventors have found that the compound of aluminate ions and soluble silica is precipitated in the water to be treated, so that the soluble silica contained in the water to be treated can be removed from the water to be treated more efficiently than before. The present invention has been completed.

  Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings. In addition, this invention is not limited to each following embodiment, It can implement by changing suitably. Further, the following embodiments can be implemented in combination as appropriate.

(First embodiment)
FIG. 1 is a schematic view of a water treatment apparatus 1 according to the first embodiment of the present invention. As shown in FIG. 1, the water treatment device 1 according to the present embodiment adds a pH adjusting agent 11a to the water to be treated W1 containing soluble silica and sets the pH of the water to be treated W1 within a predetermined range. The aluminate ion addition part which makes the density | concentration of the aluminate ion of the to-be-processed water W1 the predetermined range by adding the aluminate ion additive represented by following General formula (1) to the regulator addition part 11 and the to-be-treated water W1 12, a soluble silica precipitation portion 13 for precipitating soluble silica from the water to be treated W1 having a pH within a predetermined range and a concentration of aluminate ions, and the water from the water to be treated W1 and the water to be treated W1. The solid-liquid separation part 14 which obtains the treated water W2 by solid-liquid separation of the dissolved silica, and the treated water W1 from which the soluble silica is separated by the solid-liquid separation part 14 are filtered to treat the treated water W2 and the concentrated water. Equipped with W3 reverse osmosis membrane filtration unit 30 That. The addition amount of the pH adjuster 11 a from the pH adjuster addition unit 11 and the addition amount of the aluminate ion additive 12 a from the aluminate ion addition unit 12 are controlled by the control device 21.
^{_{[Al (OH) 4] -}} ··· formula (1)

  Further, the water treatment apparatus 1 according to the present embodiment includes a seed material addition unit 16 that adds at least a part of the precipitate 15 separated by the solid-liquid separation unit 14 to the soluble silica precipitation unit 13 as a seed material 16a. The magnesium ion addition part 17 provided in the upstream of the pH adjuster addition part 11 is provided. The seed material addition unit 16 and the magnesium ion addition unit 17 are not necessarily provided as long as the soluble silica component in the water to be treated W1 can be precipitated.

  The treated water W1 is not particularly limited as long as it contains soluble silica. For example, cooling water (blowdown water) for cooling towers of power plants and plant facilities, waste water for semiconductor manufacturing facilities, boiler replenishment water , Wastewater containing silica from boiler make-up water production facilities, well water, hot springs, geothermal power plant condensate, hot water, industrial wastewater, mine wastewater and oil-gas associated water, sewage and treated water, seawater, Examples include flooded water and surface water. The water to be treated is preferably one having a pH of 5.5 or more from the viewpoint of efficiently precipitating soluble silica contained in the water to be treated.

  The pH adjuster addition unit 11 adjusts the pH of the water to be treated to a predetermined range by adding pH adjusters 11a such as various acids and various bases to the water to be treated W1. Examples of the pH adjuster include various acids such as hydrochloric acid, sulfuric acid, and citric acid, and various bases such as sodium hydroxide and calcium hydroxide. The pH of the water to be treated W1 is not particularly limited as long as the soluble silica contained in the water to be treated W1 can be precipitated.

The aluminate ion addition unit 12 adds the aluminate ion additive represented by the general formula (1) to the water to be treated W1. By adding this aluminate ion additive to the water to be treated W1, a compound of the aluminate ion additive and soluble silica contained in the water to be treated W1 (for example, Mg ₅ Al [AlSi ₃ O ₁₀ ( OH) ₂ ] (OH) ₆ , NaAlO _2. (SiO ₂ ) _3, etc.) are deposited, so that the soluble silica contained in the water to be treated W1 can be efficiently removed.

  The aluminate ion additive is not particularly limited as long as it generates aluminate ions in the water to be treated W1. For example, sodium aluminate (sodium tetrahydroxide aluminate), lithium aluminate, sodium aluminate, Examples include various aluminates such as potassium aluminate, strontium aluminate, calcium aluminate and magnesium aluminate, and water containing aluminate ions. Among these, sodium aluminate is preferable from the viewpoint of removal efficiency of soluble silica in the water to be treated W1.

  The structure of the soluble silica precipitation part 13 will not be restrict | limited especially if soluble silica can be precipitated. The soluble silica precipitation part 13 may have, for example, a mixing tank provided with a predetermined stirring device, or may not have a mixing tank. In the soluble silica precipitation part 13 which has a mixing tank, an aluminate ion additive is added to the water to be treated whose pH is adjusted to a predetermined range in the mixing tank as necessary, and mixed by stirring to precipitate soluble silica. Let As a result, the aluminate ion additive is rapidly and uniformly mixed, and the soluble silica precipitates in about several seconds to several tens of seconds without agglomeration of the reaction time between the aluminate ions and the silica. The stirring speed may be a slow stirring or a rapid stirring. By rapidly stirring at a stirring speed of 100 rpm or more, the volume of the mixing tank can be reduced. Moreover, in the soluble silica precipitation part 13 which does not have a mixing tank, piping is performed by carrying out a line chemical injection and line mixing of the aluminate ion additive from the branch pipe provided in the piping through which the to-be-processed water W1 flows. Mix in. In this case, stirring efficiency can be improved by providing a member that disturbs the flow, such as a static mixer or an elbow, in the pipe.

  In the present embodiment, precipitation of soluble silica means that a compound of soluble silica and aluminate ions is precipitated as a solid from the liquid. Here, as a form of precipitation, the compound of soluble silica and aluminate ions may be precipitated as amorphous or may be precipitated as crystals. Moreover, the soluble silica precipitation part 13 may use a flocculant in order to accelerate | stimulate the solid-liquid separation of soluble silica and the to-be-processed water W1. Examples of the flocculant include aluminum salts, iron salts, and polymer flocculants.

Here, the solubility of the soluble silica (SiO ₂ ) in the water to be treated in the water treatment apparatus 1 according to the present embodiment will be described. FIG. 2 is a graph showing the relationship between the pH of water to be treated and the solubility of soluble silica in the water to be treated. In FIG. 2, the aqueous solution containing soluble silica is diluted to a predetermined SiO ₂ concentration at 25 ° C. under alkaline conditions, and then the SiO ₂ is precipitated when acid is added to lower the pH. The observed results are shown. As shown in FIG. 2, in the water treatment apparatus 1 according to the present embodiment, the SiO ₂ concentration at which the soluble silica is precipitated is minimized when the pH of the water to be treated is 9, and the pH is less than 9 or the pH is When it exceeds 9, the SiO ₂ concentration at which soluble silica precipitates tends to increase.

  FIG. 3 is an explanatory diagram showing the solubility of soluble silica in the presence of aluminate ions. In the example shown in FIG. 3, the pH is changed in the state of 200 mg / L, which is a saturated solution of soluble silica at pH 9 shown in FIG. The straight line L in FIG. 3 shows the saturated solubility of sodium aluminate as the aluminate ion additive. As shown in FIG. 3, the solubility (logarithmic display) of sodium aluminate is proportional to pH, and the solubility of sodium aluminate increases as the pH increases (see line L in FIG. 3). Here, in the presence of aluminate ions, the soluble silica remains in a dissolved state when the pH of the water to be treated W1 is 11 or 12, but the soluble silica is precipitated as a precipitate at pH 10. That is, in the presence of aluminate ions, the soluble silica is deposited as a precipitate even in a state below the saturation solubility of the soluble silica shown in FIG. 2 (see point P1 in FIGS. 2 and 3). This result is considered because sodium aluminate and soluble silica formed a compound, so that the solubility of soluble silica was lowered and the compound of sodium aluminate and soluble silica was precipitated as a precipitate.

FIG. 4A is a diagram showing the relationship between the pH of treated water W1 after addition of aluminum ions and the concentration of SiO ₂ , and FIG. 4B shows the pH of treated water W1 after addition of aluminum ions and the removal rate of SiO ₂ . It is a figure which shows the relationship. 4A and 4B show an example in which the concentration of SiO _{2 in} the water to be treated is 40 mg / L at a temperature of 25 ° C., and the aluminum concentrations are 10 mg / L, 30 mg / L, and 60 mg / L. Yes. As shown in FIGS. 4A and 4B, with the aluminum concentration in the water to be treated is for the case is 10mg / L, 30mg / L in a concentration of SiO ₂ in the treated water W1 is greatly reduced, SiO ₂ It can be seen that the removal rate is significantly improved. Further, it can be seen that the aluminum concentration in the treated water W1 equivalent concentrations of SiO ₂ and the removal rate can be obtained and if it is the case with 60 mg / L is 30 mg / L. From this result, the removal effect of soluble silica is obtained when the concentration of aluminum in the water to be treated W1 is 10 mg / L or more. From the viewpoint of the removal efficiency of soluble silica and the aluminate ion additive added as necessary From the viewpoint of reducing the amount used, it is found that 20 mg / L or more is preferable and 30 mg / L or more is more preferable.

Further, when the pH of the water W1 to be treated after the addition of aluminum ions is less than 5.5, the concentration of SiO ₂ tends to be high. On the other hand, when the pH is 5.5 or more, the concentration of SiO ₂ Decreases rapidly to 25 mg / L or less, and the removal rate of SiO ₂ increases rapidly. Then, the again the concentration of SiO ₂ exceeds pH9 increases, it is found that the tendency for removal rate of SiO ₂ is reduced. This result, aluminate ions, in pH5.5 or less is present as Al3 +, Al _{(OH) 4} at pH5.5 or higher ^- as there as in the range of more than pH5.5, Al _{(OH) 4} ^- This is probably because a compound of silica and soluble silica (SiO ₂ ) was formed. Considering the above, from this result, the pH of the water to be treated W1 is preferably 5.5 or more, more preferably 6 or more, from the viewpoint of efficiently reducing the concentration of soluble silica in the water to be treated W1. 7 or more is more preferable, 8 or more is more preferable, 13 or less is preferable, 12 or less is more preferable, 11 or less is still more preferable, and 10.5 or less is still more preferable. Considering the above, the pH range is preferably 5.5 or more and 12 or less, more preferably 7 or more and 11 or less, and still more preferably 8 or more and 10 or less.

FIG. 5 is a diagram showing the relationship between the aluminum concentration ratio (mol Al / mol SiO ₂ ) and the SiO ₂ removal rate in the water treatment apparatus 1 according to the present embodiment. In addition, in the example shown in FIG. 5, it has shown about the case where pH of to-be-processed water is 8, 9, and 10. As shown in FIG. 5, in the water treatment apparatus 1 according to the present embodiment, the removal ratio of SiO ₂ is about 60% when the aluminum concentration ratio is about 0.6 (mol Al / mol SiO ₂ ). When the aluminum addition rate is 1.0 or more, the SiO ₂ removal rate is drastically improved, and when the aluminum addition rate is 1.7 (mol Al / mol SiO ₂ ), it becomes 90%. Then, it can be seen that maintain the aluminum doping ratio is further removal rate of high SiO ₂ be increased.

In the water treatment apparatus 1 according to the present embodiment, as the aluminate ion concentration ratio with respect to the water to be treated, from the viewpoint of the removal rate of dissolved silica and the viewpoint of reducing the use amount of the aluminate ion additive, dissolved silica is used. On the other hand, the aluminum ion concentration ratio (mol Al / mol SiO ₂ ) is preferably 0.5 or more, more preferably 1.0 or more, further preferably 1.5 or more, and preferably 5.0 or less, 4.0. The following is more preferable, and 3.0 or less is more preferable.

The solid-liquid separation unit 14 performs solid-liquid separation of the compound of aluminate ions and soluble silica precipitated in the soluble silica precipitation unit 13 and the water to be treated W1 to obtain the treated water W2 and the precipitate 15. The solid-liquid separation unit 14 is not particularly limited as long as the solid (precipitate 15) precipitated in the water to be treated W1 and the water to be treated W1 can be solid-liquid separated. Examples of the solid-liquid separation unit 14 include a clarifier, a liquid cyclone, a sand filtration, and a membrane separation device. Examples of the precipitate 15 include silica compounds such as Mg ₅ Al [AlSi ₃ O ₁₀ (OH ₂ )] (OH) ₆ and NaAlSi ₃ O ₈ based on silica, aluminum, and magnesium contained in the water to be treated. , Aluminum compounds and magnesium compounds.

  In the present embodiment, it is preferable to use a liquid cyclone as the solid-liquid separation unit 14. As a result, it is possible to separate the precipitates for each particle size, so that it is possible to use a precipitate having an appropriate particle size as the seed material 16a to be added in the seed material addition unit 16 described later, and to dissolve efficiently. It is possible to deposit a functional silica component.

In the solid-liquid separation unit 14, a flocculant may be used to promote solid-liquid separation. Examples of the flocculant include iron-based flocculants and polymer flocculants. Among these, from the viewpoint of efficiently removing aluminate ions, it is preferable to use an iron-based flocculant (FeCl ₃ or the like).

In the present embodiment, the seed material addition unit 16 includes Mg ₅ Al [AlSi ₃ O ₁₀ (OH ₂ )] (OH) ₆ and NaAlSi ₃ O ₈ that are precipitates separated by the solid-liquid separator 14. The Si—Al compound is added as a seed material when the soluble silica component is precipitated from the water to be treated W1. By adding this seed substance, the precipitation rate of the soluble silica component from the water to be treated W1 can be increased, so that the soluble silica component can be quickly precipitated from the water to be treated W1. The processing amount of W1 is improved. In the present embodiment, the example in which the seed material 16a is added to the soluble silica precipitation portion 13 has been described. However, if the seed material 16a is on the upstream side of the soluble silica precipitation portion 13, the soluble silica precipitation is not necessarily performed. It is not necessary to add it in the part 13.

The magnesium ion addition part 17 adds the magnesium ion additive 17a in the to-be-processed water W1, and makes the magnesium ion density | concentration in the to-be-processed water W1 into a predetermined range. Thus, it is possible to moderate range of magnesium ion concentration in the treated water W1, the precipitation in the soluble silica deposition unit 13, for _{example, Mg 5 Al [AlSi 3 O} 10 (OH 2)] ( Mg—Al—Si compounds such as OH) ₆ are efficiently formed, and the concentration of dissolved silica in the treated water W2 can be further reduced. Further, the concentration of aluminum ions remaining in the treated water W2 can be reduced. The addition amount of the magnesium ion additive 17a is controlled by the control device 21 via the valve V3.

FIG. 6A is a diagram showing the relationship of the concentration of SiO _{2 in} the treated water after the addition of magnesium ions, and FIG. 6B is a diagram showing the relationship of the removal rate of SiO _{2 in} the treated water after the addition of aluminum ions. . In the example shown in FIGS. 6A and 6B, dissolution is performed when aluminum ions and magnesium ions are added to the water to be treated W1 having a temperature of 25 ° C., a pH of 9 to be treated, and a concentration of soluble silica of 40 mg / L. The concentration of silica and the removal rate are shown.

  As shown in FIG. 6A and FIG. 6B, no significant difference is found in the concentration and removal rate of soluble silica under the condition that the aluminum ion is 0 mg / L, regardless of whether the magnesium concentration is 0 mg / L or 120 mg / L. On the other hand, under the condition where the aluminum ion is 30 mg / L, the concentration of soluble silica is greatly reduced even when the magnesium concentration is 0 mg / L. However, the concentration of soluble silica is further increased by setting the magnesium concentration to 120 mg / L. As it decreases, the removal rate increases. This result is considered to be due to the synergistic effect that the precipitation of soluble silica was promoted by the formation of the Mg-Al-Si compound described above due to the coexistence of aluminum ions and magnesium ions.

  Examples of the magnesium ion additive 17a include various magnesium salts such as magnesium oxide, magnesium hydroxide, magnesium alkoxide, magnesium acetate, magnesium carbonate, magnesium chloride, and magnesium sulfate. Among these, it is preferable to use an aqueous solution of magnesium sulfate from the viewpoint of efficiently depositing soluble silica.

  The magnesium ion concentration in the water to be treated W1 is 60 mg / L or more, so that the effect of removing soluble silica is obtained. From the viewpoint of the removal efficiency of soluble silica and the use amount of the aluminate ion additive added as necessary. From the viewpoint of reduction, it is understood that 90 mg / L or more is preferable, and 120 mg / L or more is more preferable.

The magnesium ion content in the water to be treated W1 is preferably such that the magnesium concentration (Mg / SiO ₂ ) is more than 0 with respect to the soluble silica from the viewpoint of efficiently depositing the soluble silica. 0.5 or more, preferably 3 or more, more preferably 10 or less, more preferably 7 or less, and still more preferably 5 or less.

The electrolysis unit 18 electrolyzes water into electrolyzed water W4. The electrolysis unit 18 includes an anode 18a made of aluminum, a cathode 18b made of titanium or aluminum, and a DC power source 18c provided between the anode 18a and the cathode 18b. In the electrolysis unit 18, aluminum ions (Al ³⁺ ) are generated based on the following reaction formula (2) at the anode 18a, and hydroxide ions (OH ⁻ ) are generated based on the following reaction formula (3) at the cathode 18b. Generate. Thereby, in this electrolysis part 18, since the following reaction formula (4) aluminum ions and hydroxide ions react to generate aluminate ion-containing water, the electrolysis part 18 becomes a supply source of aluminate ions. . By supplying this aluminate ion-containing water as the aluminate ion additive 12a to the aluminate ion addition unit 12, it is possible to supply the aluminate ion additive without using any other aluminate ion additive. Become. As water electrolyzed in the electrolysis part 18, the to-be-processed water W1, the treated water W2, the concentrated water W3, etc. can be used, for example. The electrolysis unit 18 is not necessarily provided.
Al → Al ³⁺ + 3e ⁻ (2)
2H ₂ O + 2e ⁻ → H ₂ + 2OH ⁻ (3)
Al ³⁺ + 4OH ⁻ → [Al (OH) ₄ ] ⁻ (4)

  In the electrolysis unit 18, the anode 18a and the cathode 18b may each be an aluminum electrode. Thereby, aluminum ions can be generated from each of the anode 18a and the cathode 18b by switching the positive electrode and the negative electrode of the DC power supply 18c and inverting the polarity.

  The reverse osmosis membrane filtration unit 30 is a reverse osmosis membrane device (RO) provided with a reverse osmosis membrane 30a. The reverse osmosis membrane filtration unit 30 allows the treated water W1 from which the soluble silica has been removed to pass through the reverse osmosis membrane 30a and supply it as treated water W2, and discharges the concentrated water W3.

  In addition, in the water treatment apparatus 1, as long as the to-be-processed water W1 can be refine | purified, you may use the to-be-treated water purification apparatuses other than the reverse osmosis membrane filtration part 30. FIG. Examples of the water to be treated purification device include a nanofiltration membrane (NF), an electrodialyzer (ED), a polarity-changing electrodialyzer (EDR), an electric regenerative pure water device (EDI), and an electrostatic desalting device ( CDl), an evaporator, a deposition apparatus, an ion exchange resin, and the like can be used.

  The control device 21 is realized using, for example, a general purpose or dedicated computer such as a CPU (Central Processing Unit), a ROM (Read Only Memory), a RAM (Random Access Memory), and a program operating on the computer. The control device 21 adjusts the opening of the valve V1 based on the pH of the water to be treated W1 measured by the pH meter 22 and changes the amount of the pH adjuster 11a added to the water to be treated W1 to change the amount of the water to be treated W1. Control the pH. Moreover, the control apparatus 21 adjusts the opening degree of valve | bulb V2 based on the aluminum concentration in the to-be-processed water W1 measured with the aluminum concentration meter 31, and changes the addition amount of the aluminate ion additive 12a with respect to the to-be-processed water W1. Thus, the aluminum ion concentration in the water to be treated W1 is controlled. Further, the control device 21 adjusts the opening degree of the valve V3 based on the aluminum concentration in the treated water W1 measured by the aluminum concentration meter 31, and changes the addition amount of the magnesium ion additive 17a to the treated water W1. Thus, the magnesium ion concentration in the water to be treated W1 is controlled. Furthermore, the control device 21 controls the addition amount of the flocculant in the soluble silica precipitation portion 13 based on the aluminum concentration in the water to be treated W <b> 1 measured by the aluminum concentration meter 31.

  Next, the overall operation of the water treatment apparatus 1 according to the present embodiment will be described. To-be-treated water W1 (for example, pH 6.5) containing soluble silica such as cooling water for plant equipment has a predetermined magnesium ion concentration to which the magnesium ion additive 17a is added from the magnesium ion addition unit 17 as required. After being within the range, the pH adjuster 11a is added from the pH adjuster adding unit 11 as necessary, and the pH is controlled within a predetermined range (for example, pH 8 or more and 10 or less). Then, the aluminate ion additive 12a is added to the to-be-processed water W1 from the aluminate ion addition part 12 in the soluble silica precipitation part 13 as needed. Thereby, since the aluminate ion density | concentration and pH are adjusted in the predetermined range, the to-be-processed water W1 precipitates a soluble silica in the soluble silica precipitation part 13. FIG. Here, the control device 21 controls the valve V1 so that the pH of the water to be treated W1 introduced into the solid-liquid separation unit 14 is in a predetermined range (for example, pH 8 to 10) and the magnesium ion concentration is in the predetermined range. , V3 opening degree is controlled.

  Thereafter, the water to be treated W1 is introduced into the solid-liquid separation unit 14, and after the precipitate 15 is removed by a membrane filtration device or the like, it is filtered by the reverse osmosis membrane filtration unit 30 and separated into the treated water W2 and the concentrated water W3. Is done. Here, the control device 21 controls the amount of aluminate ions added by controlling the opening of the valve V2 so that the aluminum ion concentration in the treated water W1 measured by the Al concentration meter 31 falls within a predetermined range. To do.

  As described above, according to the water treatment apparatus 1 according to the present embodiment, the aluminate ion additive 12a is added to the water to be treated W1 containing soluble silica, so the soluble silica in the water to be treated. Precipitates without being aggregated in the water to be treated W1. This makes it possible to efficiently reduce the concentration of soluble silica in the water to be treated compared with the case where the flocculant is added to the water to be treated to remove the soluble silica. The water treatment apparatus 1 that can efficiently remove the soluble silica can be realized. And since the aluminate ion additive 12a is added based on the aluminum ion concentration in the to-be-processed water W1 measured by Al concentration meter 31 provided in the entrance of the reverse osmosis membrane filtration part 30, a reverse osmosis membrane filtration apparatus It is possible to prevent the influence of aluminum ions on the 30 reverse osmosis membranes 30a, and it is also possible to prevent the reverse osmosis membrane 30a from being deteriorated.

  In the present embodiment, the example in which the pH of the water to be treated W1 is adjusted within the predetermined range by the pH adjuster addition unit 11 has been described. However, when the water to be treated W1 having a pH within the predetermined range is used in advance. The pH adjuster addition unit 11 is not necessarily provided. In the present embodiment, the example in which the concentration of aluminate ions in the water to be treated W1 is adjusted within the predetermined range by the aluminate ion adding unit 12 has been described. When using water W1, the aluminate ion addition part 12 does not necessarily need to be provided.

By the way, when processing a to-be-processed water with a reverse osmosis membrane filtration apparatus, obstruction | occlusion of the reverse osmosis membrane based on the scale of aluminum by precipitation of aluminum hydroxide (Al (OH) ₃ ) based on an aluminum ion may arise. . In this case, scale precipitation and clogging may easily occur due to the reduction of the amount of treated water by the reverse osmosis membrane filtration device and the concentration of the local treatment plant of the reverse osmosis membrane filtration membrane due to the increase in the supply pressure of the treated water. is there.

  In water treatment equipment including reverse osmosis membrane filtration equipment, chlorine radicals such as hypochlorous acid (NaClO) remain, or chlorine such as hypochlorous acid is added to control the microorganism concentration by sterilization There is. These chlorines are generally removed by reduction treatment with a reducing agent and adsorption by activated carbon, but if chlorine roots remain in the treated water introduced into the reverse osmosis membrane where the chlorine roots cannot be treated, The reverse osmosis membrane is electrically destroyed by chlorine, resulting in a decrease in the amount of reverse osmosis membrane permeate and a decrease in the desalination rate. Here, when a metal such as aluminum ion is present, the destruction of the membrane surface of the reverse osmosis membrane may be accelerated by the catalytic effect of the metal.

Furthermore, in the reverse osmosis membrane filtration device, by adding a scale inhibitor upstream of the reverse osmosis membrane filtration device, the adhesion of calcium-based scale (gypsum: CaSO ₄ , calcium carbonate: CaCO ₃ ) to the reverse osmosis membrane is prevented. However, when aluminum ions are present in the water to be treated, the effectiveness of the scale inhibitor may deteriorate. For these reasons, aluminum-based chemicals (sulfuric acid bands, PAC polyaluminum chloride, sodium aluminate, etc.) are generally not used in water treatment devices that use reverse osmosis membranes, and iron-based chemicals. (Eg iron chloride FeCl ₃ etc.) is generally used.

  The present inventors provide solubility by providing an aluminum ion treatment part for precipitating aluminum in the water to be treated W1 from which the soluble silica has been removed, after the soluble silica precipitation part 13 of the water treatment apparatus 1 described above. It has been found that adverse effects on the reverse osmosis membrane filtration device based on aluminum ions in the water to be treated W1 from which silica has been removed can be reduced.

(Second Embodiment)
FIG. 7 is a schematic view of a water treatment device 2 according to the second embodiment of the present invention. As shown in FIG. 7, the water treatment device 2 according to the present embodiment is provided at the subsequent stage of the solid-liquid separation device 14, and an Al treatment unit 33 that treats aluminum ions in the water to be treated W1, and the Al treatment unit A pH adjuster addition unit 32 is provided in a subsequent stage of 33 to adjust the pH of the water to be treated W1 by adding the pH adjuster 32a to the water to be treated W1. Other configurations are the same as those of the water treatment apparatus 1 shown in FIG.

  The Al treatment unit 33 precipitates aluminum ions in the water to be treated W1 as an aluminum compound 34 using a chelate resin, an ion exchange resin, a chelating agent, or the like. Thereby, since the density | concentration of the aluminum ion in the to-be-processed water W1 can be reduced, the bad influence based on the aluminum ion to the reverse osmosis membrane filtration part 30 provided in the back | latter stage can be reduced. As the ion exchange resin, for example, various anion exchange resins and various cation exchange resins can be used in appropriate combination. As the anion exchange resin, a strong basic anion resin or a weak basic anion resin may be used. Further, as the cation exchange resin, a strong acid cation exchange resin or a weak acid anion exchange resin may be used.

  In the Al process part 33, the density | concentration of the aluminum ion in the to-be-processed water W1 from which the soluble silica was removed by the following 1st process methods-the 4th process method is reduced. As the first treatment method, after adjusting the pH of the water to be treated W1 from which the soluble silica has been removed to a predetermined range, the saturation solubility of the aluminum ions is lowered, and the aluminum ions in the water to be treated W1 are insolubilized. A precipitation method in which solid-liquid separation and aluminum ions are performed can be used.

  As the second treatment method, there is a chelate resin method in which water to be treated W1 is passed through a chelate resin tower in which a tubular member is filled with a chelate resin, and a heavy metal such as aluminum is adsorbed on the chelate resin to remove aluminum ions. Can be mentioned.

  As a third treatment method, a liquid chelating agent such as a flocculant is added to the water to be treated W1, and a heavy metal such as aluminum is precipitated as an insoluble chelate complex in the water to be treated W1, followed by solid-liquid separation. A liquid chelate method for removing aluminum ions can be mentioned.

As a 4th processing method, as shown to following formula (5)-following formula (7), slaked lime (Ca (OH) ₂ ) is added in the to-be-processed water W1, and the pH of the to-be-processed water W1 is increased. In addition, by supplying calcium ions and hydroxide ions, calcium carbonate (CaCO ₃ ) is precipitated from bicarbonate ions (HCO ₃ ⁻ ) contained in the water to be treated W1 and hydroxylated from magnesium ions (Mg ²⁺ ). A cold dry method in which magnesium (Mg (OH) ₂ ) is precipitated and solid-liquid separated can be used. In this cold dry method, a part of aluminum ions is also coprecipitated and removed.
Ca (HCO ₃ ) ₂ + Ca (OH) ₂ → 2CaCO ₃ ↓ + 2H ₂ O (5)
Mg (HCO ₃ ) ₂ + 2Ca (OH) ₂ ⇒Mg (OH) ₂ ↓ + 2CaCO ₃ ↓ + 2H ₂ O (6)
CaCl ₂ + Na ₂ CO ₃ ⇒2NaCl + CaCO ₃ ↓ (7)

  When the first, third, and fourth processing methods are performed, the Al processing unit 33 may be provided with a solid-liquid separation device that is separate from the solid-liquid separation unit 14 provided in the subsequent stage. preferable. By providing a solid-liquid separation device separately from the solid-liquid separation unit 14, the aluminum compound 34 can be solid-liquid separated.

  In the Al treatment unit 33, a water treatment additive such as a scale inhibitor may be added to the water to be treated W1. Thereby, since the saturation solubility of the aluminum ion with respect to the to-be-processed water W1 can be improved, the bad influence based on the aluminum ion to the reverse osmosis membrane 30a of the reverse osmosis membrane filtration part 30 provided in the back | latter stage can be reduced.

  The pH adjusting device 32 improves the saturation solubility of aluminum ions in the water to be treated W1 by adding a pH adjusting agent 32a to the water to be treated W1 from which the soluble silica has been removed to reduce or increase the pH of the water to be treated W1. Let Examples of the pH adjuster 32a include various acids such as hydrochloric acid, sulfuric acid, and citric acid, and various bases such as sodium hydroxide and calcium hydroxide. The control device 21 adjusts the addition amount of the pH adjusting agent 32a by adjusting the opening degree of the valve V4 based on the measured value of the pH meter 23 provided at the subsequent stage of the solid-liquid separator 14. Thereby, since the saturation solubility of the aluminum ion with respect to the to-be-processed water W1 can be improved, the bad influence based on the aluminum ion to the reverse osmosis membrane filtration part 30 provided in the back | latter stage can be reduced.

  When the alkali is added to the water to be treated W1 to increase the saturation solubility of aluminum, the pH adjusting device 32 preferably increases the pH of the water to be treated W1 by more than 0, and may be increased by +0.1 or more. More preferably, it is further increased by +0.3 or more, and more preferably by +1.0 or more. In addition, when the pH adjusting device 32 increases the saturation solubility of aluminum by adding an acid to the water to be treated W1, for example, if the pH of the water to be treated W1 is 9, the pH of the water to be treated W1 is adjusted. By setting it to 4.2 or less, the saturation solubility of aluminum can be increased. For example, when the aluminum concentration in the water to be treated W1 is about 0.01 mg / L, the pH adjusting device 32 can control the pH of the water to be treated W1 by 5.0 or less and 6.0 or more. Precipitation can be prevented.

  For example, when the pH of the discharged water from the solid-liquid separation unit 14 is 9, the pH adjusting device 32 adjusts the pH to a range of 4.5 or more and 9 or less to remove excess aluminum from the water to be treated W1. It can be deposited. Since the solubility of aluminum ions is minimized when the pH is 5.5, by adjusting the addition amount of the pH adjusting agent 32a to adjust the pH to pH 4.5 or more and 9 or less, excess aluminum can be converted into an aluminum compound. As 34, it precipitates from the for-treatment water W1. The precipitated aluminum compound 34 can be removed together with the precipitate 15 by the solid-liquid separation unit 14. In this case, the pH of the water to be treated W1 is pH 4.8 or more and 7.0 from the viewpoint of setting the aluminum concentration in the water W1 to be treated introduced into the reverse osmosis membrane filtration unit 30 to 0.05 mg / L or less. From the viewpoint of setting the aluminum concentration in the water to be treated W1 introduced into the reverse osmosis membrane filtration unit 30 to 0.01 mg / L or less, a range of pH 5.0 or more and 6.0 or less is more preferable.

  Next, the overall operation of the water treatment device 2 according to the present embodiment will be described. First, the precipitate 15 is removed from the to-be-processed water W1 similarly to the water treatment apparatus 1 mentioned above. Thereafter, in the water to be treated W1 from which the precipitate 15 has been separated, aluminum ions are removed by the Al treatment unit 33 using a chelate resin, an ion exchange resin, a chelating agent, or the like. Here, the Al processing unit 33 may add a scale inhibitor to increase the solubility of aluminum ions. Thereafter, the water to be treated W1 is separated into treated water W2 and concentrated water W3 by the reverse osmosis membrane filtration unit 30 after the pH adjusting agent 32a is added by the pH adjusting agent adding unit 32 and the pH is adjusted to a predetermined range. The Here, the control device 21 adds the amount of ions such as a chelating agent and ions so that the aluminum ion concentration in the treated water W1 measured by the Al concentration meter 31 falls within a predetermined range (for example, 0.01 mg / L). Controls processing of exchange resin. Moreover, the control apparatus 21 may control the addition amount of the aluminate ion added to the precipitation tank 13, and may reduce the aluminum ion concentration introduce | transduced into the reverse osmosis membrane filtration part 30. FIG.

  Thus, according to this Embodiment, since the aluminum ion of the to-be-processed water W1 is reduced by the Al process part 33 provided in the back | latter stage of the solid-liquid separation part 14, compared with the water treatment apparatus 1 mentioned above. The aluminum ion concentration of the for-treatment water W1 introduced into the reverse osmosis membrane filtration unit 30 can be further reduced. Thereby, the influence of aluminum ions on the reverse osmosis membrane 30a of the reverse osmosis membrane filtration unit 30 can be further reduced.

(Third embodiment)
FIG. 8 is a schematic view of a water treatment device 3 according to the third embodiment of the present invention. As shown in FIG. 8, in the water treatment device 3 according to the present embodiment, the Al treatment unit 33 of the water treatment device 2 described above is provided between the soluble silica precipitation unit 13 and the solid-liquid separation unit 14. Yes. Since other configurations are the same as those of the water treatment apparatus 2 described above, description thereof is omitted.

  As described above, according to the present embodiment, aluminum is precipitated by the Al treatment unit 33 and the aluminum ions are removed together with the precipitate 15 by the solid-liquid separation unit 14. The aluminum ion concentration of the to-be-processed water W1 introduce | transduced into the osmosis membrane filtration part 30 can be reduced more. Thereby, it becomes possible to further reduce the influence of aluminum ions on the reverse osmosis membrane 30a of the reverse grooming membrane filtration unit 30.

  In the sixth embodiment, the configuration in which the Al processing unit 33 is provided in the subsequent stage of the solid-liquid separation unit 14 will be described. In the seventh embodiment, the Al processing unit 33 is replaced with the solid-liquid separation unit. Although the configuration provided in the front stage of 14 has been described, the Al processing unit 33 may be provided in both the front stage and the rear stage of the solid-liquid separation unit 14. Thereby, after reducing the aluminum ion concentration in the to-be-processed water W1 by the Al process part 33 provided in the front | former stage of the solid-liquid separation part 14, after isolate | separating the precipitate 15 in the solid-liquid separation part 14, it is further soluble. Since the aluminum ions in the water to be treated W1 from which the silica has been removed can be removed as the aluminum compound 34, the concentration of aluminum ions supplied to the treated water purification unit 20 can be further reduced.

  Hereinafter, application examples of the water treatment apparatus according to the above embodiment will be described. In the following, an example in which the soluble silica removing unit 10 shown in FIG. 9 is applied to various water treatment apparatuses will be described. As shown in FIG. 9, the soluble silica removing unit 10 includes a pH adjuster adding unit 11 for adding a pH adjuster 11a to the water to be treated W1 and a water to be treated W1 to which the pH adjuster 11a has been added. The aluminate ion addition part 12 which adds the aluminate ion additive 12a, the soluble silica precipitation part 13 which precipitates the soluble silica in the to-be-processed water W1 which added the aluminate ion, and the precipitated soluble silica And a solid-liquid separation unit 14 that obtains treated water W2 by solid-liquid separation.

(Application example 1)
FIG. 10 is a schematic diagram of the water treatment apparatus 100 according to Application Example 1. As shown in FIG. 10, this water treatment apparatus 100 is a pretreatment apparatus for feed water of a high purity water refining reverse osmosis plant for semiconductor production. The water treatment apparatus 100 removes bicarbonate and aluminum ions by treating the treated water W2 with a weak acid cation exchange resin and the soluble silica removing unit 10 that removes the soluble silica in the treated water W1. A cation exchange device 101 as a water purification device, a decarboxylation unit 102 for removing carbon dioxide in the treated water W2 from which bicarbonate and aluminum ions have been removed, and the decarboxylated treated water W2 are filtered by a reverse osmosis membrane 103a. A reverse osmosis membrane filtration unit 103 for obtaining permeated water W100 and concentrated water W101.

The permeated water W100 that has passed through the reverse osmosis membrane filtration unit 103 is further purified by an ion exchange resin 104 such as a cation exchange device or an anion exchange device. Irradiated to kill organisms and used as purified treated water W102. Between the soluble silica removal unit 10 and the cation exchange device 101, _Na 2 CO ₃ supply unit 107 supplies the _Na 2 CO ₃ water to be treated W1 is provided solubility silica was removed. Between the cation exchange apparatus 101 and the decarboxylation part 102, the acid supply part 108 which supplies an acid to the to-be-processed water W1 refine | purified by ion exchange is provided. Between the decarboxylation unit 102 and the reverse osmosis membrane filtration unit 103, an alkali supply unit 109 that supplies alkali to the decarboxylated water to be treated W1 is provided. In addition, in this water treatment apparatus 100, if the soluble silica removal part 10 is an upstream of the reverse osmosis membrane filtration part 103, arrangement | positioning structure can be changed suitably. Thus, in this Embodiment, it is also possible to further refine | purify and use the treated water W2 processed with the soluble silica removal part 10 via the cation exchange apparatus 101 grade | etc.,.

(Application example 2)
FIG. 11 is a schematic diagram of a water treatment device 200 according to Application Example 2. As shown in FIG. 11, this water treatment device 200 is a wastewater treatment device containing a high concentration organic substance and a suspended / dissolved solid content such as silica. In this water treatment device 200, the soluble silica removing unit 10 </ b> A further includes a coagulation tank 201 for aggregating the soluble silica in the water to be treated W <b> 1 after the soluble silica precipitation unit 13. In this coagulation tank 201, the soluble silica in the to-be-processed water W1 to which the aluminate ion was added from the aluminate ion addition part 12 is deposited with coagulant | flocculants, such as iron chloride, in the to-be-treated water W1. And after isolate | separating the soluble silica which precipitated in the solid-liquid separation part 14, after obtaining the treated water W2 and the precipitate 15, it filtered with the 1st filter 202 comprised by a multimedia filter, and is contained in the treated water W2. The aluminum ions to be removed are removed by an ion exchange resin 203 as a water purification unit. And after filtering with the 2nd filter 204 comprised with a cartridge filter, the permeated water W200 and the concentrated water W201 are isolate | separated by the reverse osmosis membrane filtration part 205 provided with the reverse osmosis membrane 205a. Thus, in this Embodiment, it is also possible to generate | occur | produce and use the treated water W2 processed by the soluble silica removal part 10 via the ion exchange resin 203 grade | etc.,.

(Application example 3)
FIG. 12 is a schematic diagram of a water treatment device 300 according to Application Example 3. As shown in FIG. 12, this water treatment apparatus 300 is provided in the 1st demineralization tower 301 as a to-be-processed water refinement | purification part provided in the back | latter stage of the soluble silica removal part 10, and the back | latter stage of the desalination tower. A degassing tower 302 and a second demineralization tower 304 provided at the rear stage of the degassing tower 302 are provided. The treated water W2 introduced into the first demineralization tower 301 is ion-exchanged via the first ion exchange resin 301a and the second ion exchange resin 301b, and then hydrochloric acid is supplied at the bottom of the tower to enter the degassing tower 302. Supplied. The treated water W2 supplied to the degassing tower 302 is washed by the washing section 302a and stored in the tower bottom section 302b. The treated water W2 stored in the tower bottom 302b of the degassing tower 302 is introduced into the second demineralization tower 304 via the pump 303 and ion exchanged via the first ion exchange resin 304a and the second ion exchange resin 304b. After that, a sodium hydroxide aqueous solution is supplied at the bottom of the tower, adjusted to a predetermined pH, and treated water W300. By processing in this way, it becomes possible to reduce the consumption rate of the ion exchange resin. In addition, if the soluble silica removal part 10 is an upstream of the 2nd ion exchange resin 304b of the 2nd demineralization tower 304, arrangement | positioning structure can be changed suitably. Thus, in this application example 3, the treated water W2 treated by the soluble silica removing unit 10 can be further generated and used through an anion exchange resin or the like.

  As the first ion exchange resins 301a and 304a and the second ion exchange resins 301b and 304b of the first demineralization tower 301 and the second demineralization tower 304, various anion exchange resins and cation exchange resins may be used in appropriate combinations. it can. In this application example 3, it is preferable to use a strongly acidic cation exchange resin as the first ion exchange resin 301a and the second ion exchange resin 301b of the first demineralization tower 301, and the first ion of the second demineralization tower 304 is the first ion. As the exchange resin 304a and the second ion exchange resin 304b, it is preferable to use a strongly basic anion exchange resin.

  In addition, the structure of the water treatment apparatus 300 provided with the 1st demineralization tower 301, the degassing tower 302, and the 3rd demineralization tower 304 in the application example 3 mentioned above can be changed suitably. In the water treatment apparatus 300, the degassing tower 302 and the third demineralization tower 304 may be omitted. In this case, it is preferable that the first demineralization tower 301 includes a strongly acidic cation resin as the first ion exchange resin 301a and a strongly basic anion resin as the second cation exchange resin 301b. By comprising in this way, when the ion concentration in the to-be-processed water W1 is low, it becomes possible to obtain the treated water W300 efficiently. Even in this case, the amount of chemicals required for regeneration of the strongly basic anion resin and the amount of the strongly basic anion resin used by removing the soluble silica in the water to be treated W1 by the soluble silica removing unit 10 Can be reduced.

  Further, in the water treatment apparatus 300, a third demineralization tower that polishes the treated water W300 may be further provided after the second demineralization tower 304. In this case, it is preferable that the third desalting tower includes a strongly acidic cation resin as the first ion exchange resin and a strongly basic anion resin as the second cation exchange resin. By comprising in this way, the purity of the to-be-processed water W300 further improves. Even in this case, by removing the soluble silica in the water to be treated W1 by the soluble silica removing unit 10, the first ion exchange resins 301a, 301a of the first demineralization tower 301 and the second demineralization tower 304 are obtained. Reducing the amount of chemicals required to regenerate 304a, the strongly basic anion resin in the second ion exchange resins 301b, 304b, and the strongly basic anion resin in the third desalting tower, and the amount of the strongly basic anion resin used Can do.

(Application example 4)
FIG. 13 is a schematic diagram of a water treatment device 400 according to Application Example 4. As shown in FIG. 13, this water treatment device 400 is a water treatment device that treats water containing an organic substance and an inorganic salt to reduce scale adhesion during an evaporation operation. This water treatment device 400 includes an ion exchange device 401 provided at a subsequent stage of the soluble silica removing unit 10, an acid supply unit 402 that supplies acid to the treated water W2 ion-exchanged by the ion exchange device 401, and an ion exchange. Degassing unit 403 provided at the subsequent stage of the apparatus 401, alkali adding unit 404 for adding alkali to the treated water W2 degassed by the degassing unit 403, and water to be treated provided at the subsequent stage of the alkali adding unit 404 And an evaporator 405 as a purification unit.

  The ion exchange device 401 purifies the water to be treated W1 from which the soluble silica has been removed by ion exchange. The acid supply unit 402 adds an acid to the water to be treated W1 purified by ion exchange to bring the pH into a predetermined range. The degassing unit 403 removes carbon dioxide contained in the treated water W2. The alkali addition unit 404 adds alkali to the treated water W2 from which the carbon dioxide gas has been removed to increase the pH of the treated water W2. The evaporator 405 evaporates the basic treated water W2 to obtain the evaporated water W400, extracts the concentrated water from the bottom of the tower, and supplies it to the crystallizer 406. In the crystallizer 406, concentrated water concentrated in a range where no crystals are precipitated by the evaporator 405 is deposited, and the precipitated solid 408 is separated by the solid-liquid separation unit 407. The concentrated liquid 407 a separated by the solid-liquid separation unit 407 is supplied to the crystallizer 406 again. Thus, in this Embodiment, it is also possible to further refine | purify and use the treated water W2 processed with the soluble silica removal part 10 through the ion exchange apparatus 401, the evaporator 405, etc. FIG. Even in this case, since the soluble silica in the water to be treated W1 is reduced in the soluble silica removing unit 10, the purification efficiency of the water to be treated W1 in the ion exchange device 401 and the evaporator 405 is improved.

  Hereinafter, the present invention will be described in more detail on the basis of Examples and Comparative Examples performed to clarify the effects of the present invention. In addition, this invention is not limited at all by the following examples and comparative examples.

(Example)
Using the water treatment apparatus shown in FIG. 1, sodium aluminate was added to the water to be treated to remove soluble silica to produce purified treated water. The pH of the water to be treated was 10, the temperature was 25 ° C., the concentration of soluble silica in the water to be treated was 40 mg / L, the concentration of aluminate ions was 157 mg / L, and the magnesium ion concentration was 120 mg / L. As a result, as shown in FIG. 14, the soluble silica in the treated water was precipitated, and the concentration of the soluble silica in the treated water was greatly reduced (treated water: 40 mg / L → treated water 0.8 mg / L). ). Moreover, as a result of analyzing the composition of the precipitate by fluorescent X-ray analysis, Mg, Al, and Si coexisted in the precipitate.

(Comparative example)
The treated water was treated in the same manner as in Example except that aluminum sulfate was used in place of sodium aluminate. As a result, as shown in FIG. 14, the soluble silica in the treated water did not precipitate, and the concentration of the soluble silica in the treated water did not decrease (treated water: 32 mg / L → treated water 31 mg / L). . This result is considered to be because, when aluminum sulfate was used, aluminate ions were not generated in the treated water, and as a result, the compound of aluminate ions and soluble silica did not precipitate in the treated water.

1, 2, 3, 100, 200, 300, 400 Water treatment apparatus 10 Soluble silica removal part 11 pH adjuster addition part 11a pH adjuster 12 Aluminate ion addition part 12a Aluminate ion additive 13 Dissolvable silica Precipitation part 14 Solid-liquid separation part 15 Precipitate 16 Seed substance addition part 16a Seed substance 17 Magnesium ion addition part 17a Magnesium ion additive 18 Electrolysis part 18a Anode 18b Cathode 18c DC power supply 21 Controller 22 pH meter 30, 103, 205 Reverse Osmosis membrane filtration unit 30a, 103a, 205a Reverse osmosis membrane 31 Al concentration meter 32 pH adjuster addition unit 32a pH adjuster 33 Al treatment unit 34 Aluminum 101 Cation exchange device 102 Decarboxylation unit 201 Coagulation tank 202 First filter 203 Ion exchange Resin 204 Second filter 30 DESCRIPTION OF SYMBOLS 1 1st demineralization tower 301a, 304a 1st ion exchange resin 301b, 304b 2nd ion exchange resin 302 Decarbonation tower 302a Cleaning part 302b Tower bottom part 303 Pump 304 2nd demineralization tower 401 Ion exchange apparatus 402 Acid supply part 403 Desorption Gas part 404 Alkali addition part 405 Evaporator 406 Crystallizer 407 Solid-liquid separation part 407a Concentrated liquid 408 Solid

Claims (20)

A soluble silica precipitation part for precipitating soluble silica dissolved in the water to be treated, from the water to be treated whose aluminate ion concentration and pH represented by the following general formula (1) are within a predetermined range,
A solid-liquid separation unit for separating the treated water and the precipitated soluble silica to obtain treated water from which the soluble silica has been removed from the treated water;
A water treatment apparatus, comprising: a reverse osmosis membrane filtration unit that filters the treated water from which soluble silica has been removed in the solid-liquid separation unit with a reverse osmosis membrane.
^{_{[Al (OH) 4] -}} ··· formula (1)   The water treatment apparatus of Claim 1 provided with the aluminate ion addition part which adds an aluminate ion additive to the said to-be-processed water.   The water treatment apparatus according to claim 2, wherein the aluminate ion additive is sodium aluminate.   The water treatment apparatus of any one of Claim 1 to 3 provided with the pH adjuster addition part which adds a pH adjuster to the said treated water, and makes the said treated water pH 5.5 or more.   The water treatment according to any one of claims 1 to 4, further comprising a seed material addition unit that adds soluble silica contained in the water to be treated, which has been precipitated in advance, as a seed material to the water to be treated. apparatus.   The water treatment apparatus of any one of Claims 1-5 provided with the magnesium ion addition part which adds a magnesium ion additive to the said to-be-processed water.   The electrolyzer which adds the aluminate ion containing water generated by electrolyzing a part of the to-be-treated water to the to-be-treated water as the aluminate ion additive is provided. The water treatment apparatus according to item.   The water treatment apparatus according to any one of claims 1 to 7, further comprising an aluminum ion treatment unit that removes aluminum ions contained in the water to be treated supplied to the reverse osmosis membrane filtration unit.   The water treatment apparatus according to claim 8, wherein the aluminum ions are removed by an ion exchange resin provided in the aluminum ion treatment unit.   The water treatment apparatus according to claim 8 or 9, wherein a chelating agent is added to the water to be treated in the aluminum ion treatment unit to remove the aluminum ions. An aluminum ion concentration measuring device for measuring the aluminum ion concentration of water to be treated introduced into the reverse osmosis membrane filtration unit;
Based on the aluminum ion concentration measured by the aluminum ion concentration measuring device, the concentration of the aluminate ion, the pH of the water to be treated, the amount of the chelating agent added to the aluminum ion treatment unit, and the ion exchange resin The water treatment apparatus of any one of Claims 8-10 provided with the control apparatus which controls at least 1 of the process of these. A precipitation step of precipitating soluble silica dissolved in the treated water from the treated water in which the aluminate concentration and pH represented by the following general formula (1) are each within a predetermined range;
A solid-liquid separation step of obtaining a water to be treated from which the soluble silica is removed from the water to be treated by solid-liquid separation of the water to be treated and the precipitated soluble silica;
And a filtration step of filtering the treated water from which the soluble silica has been removed by the solid-liquid separation through a reverse osmosis membrane filtration unit.
^{_{[Al (OH) 4] -}} ··· formula (1)   The water treatment method according to claim 12, wherein an aluminate ion additive is added to the water to be treated.   The water treatment method according to claim 13, wherein the aluminate ion additive is sodium aluminate.   The water treatment method according to any one of claims 12 to 14, wherein a pH adjuster is added to the water to be treated to bring the water to be treated to pH 5.5 or more.   The water treatment method according to any one of claims 12 to 15, wherein soluble silica contained in the water to be treated that has been precipitated in advance is added to the water to be treated as a seed material.   The water treatment method according to any one of claims 12 to 16, wherein a magnesium ion additive is added to the water to be treated.   The water according to any one of claims 12 to 17, wherein aluminate-containing water generated by electrolyzing a part of the treated water is added to the treated water as the aluminate ion additive. Processing method.   The water treatment method according to any one of claims 12 to 18, wherein aluminum ions contained in the water to be treated supplied to the reverse osmosis membrane filtration unit are removed by an aluminum ion treatment unit.   Measure the aluminum ion concentration of the water to be treated introduced into the treated water purification unit, and add the aluminate ion concentration, the pH of the water to be treated, and the aluminum ion treatment unit based on the measured aluminum ion concentration The water treatment method according to any one of claims 12 to 19, wherein at least one of an addition amount of the chelating agent and a treatment of the ion exchange resin is controlled.

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